Hydrogen producing apparatus

Abstract: Disclosed is a hydrogen producing apparatus for producing hydrogen on an industrial scale through steam reforming reactions and for separating product hydrogen using a hydrogen permeable membrane, comprising nested outer, intermediate and inner cylinders, as well as a combustion burner disposed toward the inside of the inner cylinder, a catalyst layer between the intermediate and inner cylinders, hydrogen-permeable tubes disposed in the catalyst layer, and sweep gas supply tubes. The raw material gas is converted into hydrogen at a high temperature, the produced hydrogen permeates the hydrogen-permeable tube so as to be selectively separated and collected, and the hydrogen having permeated is accompanied by the sweep gas to be conducted out of the apparatus.

Description: BACKGROUND OF THE INVENTION 1. Field of the Invention This invention relates to an industrial scale hydrogen producing apparatus which manufactures hydrogen from a mixed gas of steam and either hydrocarbons or methanol through a steam reforming reaction. More specifically, this invention relates to an industrial scale hydrogen producing apparatus for obtaining hydrogen of sufficiently high purity for use in solid polymer fuel cells (polymer fuel cells) at low reaction temperatures. 2. Description of the Related Art The content of CO in hydrogen for fuel cells, in particular solid polymer fuel cells, is preferably less than 10 ppm. Hydrogen obtained from naphtha, natural gas and town gas through a steam reforming reaction has low purity and is not, as it is, suitable for fuel cells. Hydrogen obtained through steam reforming reactions is often further refined in a carbon monoxide reformer and a hydrogen refiner to boost the hydrogen purity to a desired degree. This approach to obtaining high-purity hydrogen requires complex manufacturing processes. These processes require high temperature and high pressure equipment and significant heat energy, with resultant high production cost. Hydrogen produced through such processes cannot be economically used in fuel cells. As disclosed in documents, such as Japanese Patent Provisional Publication (Kokai) No. 61-17401, proposals have been made to obtain high purity hydrogen using permeable membranes which is selectively permeable to hydrogen. The above Provisional Publication, for example, disclosed a method and an apparatus for continuously separating generated hydrogen through a selective hydrogen-permeable partitioning wall, from a reaction space which is at a temperature of 500-1000°C. This method and the required equipment can be applied to CH 4 /H 2 O reforming reactions or reactions for producing water gas. The publication explained that it is possible to separate high purity hydrogen through this method. Published documents, including the above publication, disclose a hydrogen producing apparatus on the scale of a laboratory, with its schematic chart shown in Figure 1. In the conventional hydrogen producing apparatus shown in Figure 1, reference numeral 90 indicates the reaction tube, 92 the reforming catalyst layer, and 94 the hydrogen permeation tube. The mixture of steam and hydrocarbon gas is introduced from below in the direction indicated by arrow X, reformed in the reforming catalyst layer 92, and hydrogen gas is generated. This hydrogen gas permeates the hydrogen-permeable tube 94 and flows out from the section marked with arrow Y. The reformed gas from which hydrogen has been removed flows out from the section indicated by arrow Z. These published documents disclose hardly any method or means to boost the scale of laboratory apparatuses to an industrial level. It has not yet been determined how industrial scale production can be achieved using these laboratory-level technologies. Many technical problems must be overcome to establish an economical hydrogen producing apparatus to boost the laboratory technologies for industrial-scale application. One conceivable method to create a larger apparatus would involve arranging many parallel reaction tubes equipped with hydrogen permeation tubes in the reforming catalyst layer, such as the one shown in Figure 1, and linking each inlet and outlet of these tubes with headers, so as to form a multi-tube reaction apparatus. This apparatus would have a large and complex structure, with low efficiency, low controllability and low heat efficiency. Constructing such a system would also require a large quantity of materials and would be difficult, and the equipment would thus be costly and uncompetitive. The engineering issues, such as how separation means using hydrogen-permeable membranes could be structured or how the sections for reactions could be heated, are extremely important in increasing the scale of the apparatus. However, no specific examples or solutions for these problems have been indicated. In the hydrogen from steam and methanol or propanol producing apparatus of BE-A-657241, the ingredient gas has to be heated before it is introduced into the apparatus, which requires temperatures of about 350°C or 434°C, respectively. The catalyst is heated only at the start of operation. Heating means are not incorporated into an apparatus comprising a reformation catalyst and a hydrogen-permeable membrane to form an integral apparatus. Thermal stress on the apparatus as a whole is not a problem. Some hydrocarbons generally require temperatures higher than 500°C for catalytic reformation to hydrogen. At such high temperatures, substantial thermal stresses develop. A catalytic ceramic membrane steam/hydrocarbon reformer as described in US-A-4,981,676 uses a plurality of burners heating the catalyst from the outside of the catalyst. In order to heat the catalyst uniformly and efficiently, a complicated control system for the burners must be provided for. In order to make practical use of fuel cells a reality, it is also extremely important to supply low cost, high purity hydrogen. Creating hydrogen production techniques which are capable of producing high purity hydrogen on an industrial scale at low cost has been considered as a crucial, unresolved issue. SUMMARY OF THE INVENTION Given this background, the objective of the invention as defined by the appended claims over the known reformation apparatus of BE-A-657241 is to provide an alternative industrial hydrogen producing apparatus having additional structure. The raw material gas to be introduced into the hydrogen producing apparatus according to this invention is a mixture of steam, an alcohol such as methanol, and light hydrocarbons such as natural gas, naphtha and town gas. The reforming catalyst used in this invention can be any convention catalyst for the steam reforming manufacture of hydrogen from the above mentioned raw material gas. The hydrogen producing apparatus according to this invention has a vertical furnace formed with the inner cylinder. The structure includes layered cylinders incorporating upright intermediate and outer cylinders disposed outside the inner cylinder. The apparatus has an outermost cylinder disposed outside outer, intermediate and inner cylinders. The inner annulus (including the second and third annuluses in certain cases) contains a catalyst layer filled with reforming catalyst. Installing hydrogen-permeable tubes (or double-walled hydrogen-permeable tubes in some cases) in the catalyst layer creates a reaction/separation process region. Cylindrical structures are preferable, because they ensure uniform thermal flux distribution in the radius direction within the structure of concentric, layered cylinders, with the furnace located in the center. This prevents the generation of hot spots at which temperature may exceed the limit the hydrogen permeation tubes can withstand. The raw material gas (process feed gas) is introduced into the inner annular space by means of conventional methods. The gas is modified into hydrogen when passing through the reforming catalyst layer. The hydrogen thus generated permeates the hydrogen-permeable tubes and is swept along with sweep gas, introduced from the annulus formed between the hydrogen-permeable tube and the sweep gas tube. A typical method to introduce and dissipate the process feed gas would include arranging circular pipe headers with multiple spray nozzles around the circumference of the lower section of the inner annulus. The endothermic steam reforming reaction absorbs heat, necessitating a drooping combustion burner installed in the ceiling of the internal cylinder or an upright combustion burner install on the bottom thereof. The drooping combustion burner is designed with its flames directed downward, and conventional burners can be used for this purpose. The upright combustion burner produces upwardly directed flames, and conventional burners can also be used as this type of burner. Installing a drooping combustion burner in the top section of the furnace lessens burner stains, reduces burner cleaning requirements, and simplifies inspection and maintenance. As no space needs to be provided below the burner's floor for burner inspection and maintenance, the total height of the furnace can be reduced, resulting in cost savings for the manufacture of the whole hydrogen producing apparatus. The combustion gas descends inside the inner cylinder and enters an annulus from the base of the inner cylinder. While ascending, the combustion gas heats the reforming catalyst layer in the internal annulus, and exits from the upper section of the external annulus. Heating the reforming catalyst layer from both sides ensures more uniform heating. An upright combustion burner installed in the base of the furnace will have upwardly directed flames, complying with the flame buoyancy direction and with the combustion gas flow direction, thereby improving flame stability. The combustion gas rises in the space inside the inner cylinder, then enters the top of the external annulus. As it descends, the combustion gas heats the catalyst layer in the internal annulus, and exits from the lower section of the external annulus. The internal annulus catalyst layer is also heated uniformly as heat is applied from both sides. The hydrogen-permeable tube is equipped with a hydrogen-permeable metal membrane on a porous inorganic layer. The tube selectively allows hydrogen to permeate. The reaction apparatus, incorporating the hydrogen-permeable tube, is called a membrane reactor, and this technology is already known. The double-walled hydrogen-permeable cylinders used in this invention have inner and outer walls, and are designed to make the membrane reactor more economical. Methane is employed as a typical hydrocarbon to explain the operation of the hydrogen-permeable tube. The methane reforming reaction progresses at a reaction temperature of 500-1000°C until chemical equilibrium is reached. The reaction equation is: CH 4 + H 2 O ⇄ 3H 2 + CO The conversion is encouraged at the same temperature by separating the generated hydrogen from generated products via the hydrogen-permeable tube, or by reducing the hydrogen partial pressure in the generated products, because according to the above equation, the chemical reaction proceeds further to the right hand side. In other words, the conversion efficiency can therefore be increased without a rise in reaction temperature. Although conventional methane reforming methods require a reaction temperature of about 800°C, the hydrogen producing apparatus according to this invention makes it possible to obtain the same conversion ratio at 500-600°C, utilizing hydrogen-permeable tubes or cylinders. The amount (Q H ) of hydrogen permeating per square centimeter of the hydrogen-permeable metal membrane on the hydrogen-permeable tube is proportional to the difference between the square roots of the partial pressures of hydrogen before and after passing the membrane: (Ph) 1/2 (P1) 1/2 . This means: Q H = k {(Ph) 1/2 - (P1) 1/2 }, where K is a constant. As mentioned, it is possible to shift the chemical reaction to the right hand side of the equation by collecting hydrogen using hydrogen-permeable tubes (or a hydrogen-permeable cylinder). The reforming temperature consequently can be dropped by 150-200°C, significantly improving the thermal efficiency. Also, because the reaction temperature is low, the equipment can be constructed of inexpensive materials with relatively lower thermal resistance, thereby reducing costs. Also, it should be noted that while the raw material gas flows into the catalyst layer, the sweep gas flows in the opposite direction. The hydrogen partial pressure is therefore significantly lowered because the generated hydrogen is almost completely swept in the area close to the catalyst layer outlet. Introducing the sweep gas improves the conversion efficiency of the entire reforming catalyst layer. The generated hydrogen collection efficiency is improved by the counter-current material transfer caused by the sweep gas in the hydrogen-permeable tube and reforming gas in the catalyst layer. Steam and inert gases such as nitrogen and helium can be used as the sweep gas in this hydrogen producing apparatus. The amount of hydrogen which permeates the hydrogen-permeable tube can be increased by raising the difference between the partial pressures of hydrogen on the prepermeation and after-permeation sides. This is done by circulating sweep gas on the after-permeation side to reduce the partial pressure of hydrogen. Other means to reduce the partial pressure of hydrogen on the after-permeation side include the use of a suction pump. The hydrogen-permeable metal membrane on the hydrogen-permeable tube (or double-walled hydrogen-permeable cylinders in some cases) selectively allows only hydrogen to permeate. As the hydrogen separated through the hydrogen-permeable tube is extremely pure, it is suitable for use in the solid fuel molecular cells. The 5-50 µm thick hydrogen-permeable metal membrane is formed on the inorganic porous layer, and is able to selectively permeate hydrogen. The inorganic porous layer functions as carrier to support the hydrogen-permeable metal membrane. The 0.1-1 mm thick inorganic porous layer is created from materials such as ceramic, glass, or porous stainless steel, non-woven fabric. Single or multi-layer metal mesh is incorporated in the porous layer to boost its structural strength. Although there are no restrictions on the hydrogen-permeable tube's dimensions, the most economical configuration is a 20 mm diameter cylinder. According to the first and second aspects of this invention described above, intermediate, outer and outermost upright cylinders can be nested outside the inner cylinder which forms a vertical furnace. In such an arrangement, the first and second catalyst layers are created by filling the second and third annuluses, respectively, with reforming catalyst. A reaction/separation region is created by installing a hydrogen-permeable tube in the first catalyst layer. Preferably, cylindrical vessels should be used because the structure of concentric cylinders with the furnace arranged in the center assists a uniform distribution of thermal flux in radial directions and also prevents the development of hot spots where the temperature may exceed the temperature limit of the hydrogen-permeable tube. As the raw material gas is heated, the reformation of hydrocarbons progresses in the second catalyst layer. The gas flows into the first catalyst after the temperature and the partial pressure of hydrogen reach maximum values near the catalyst layer outlet. The reforming reaction progresses further as hydrogen is extracted through the hydrogen-permeable tube. The partial pressure of hydrogen in the raw material gas significantly drops as it moves toward the outlet of the first catalyst layer. Therefore, the partial pressure of hydrogen is generally lower in the first catalyst layer. The temperature of the second catalyst layer is somewhat higher around the inner cylinder than in the first catalyst layer because the inner cylinder forms the furnace wall in the center and is heated. Thus the distribution of temperature, hydrogen partial pressure, and gas composition varies in each catalyst layer. It is therefore preferable to select catalysts which are active and durable under the conditions found in each catalyst layers. However, a catalyst suitable for both the first and second catalyst layers is actually available, a single catalyst may be used in both catalyst layers. The raw material gas (process feed gas) is introduced through the upper section of the third annulus and converted into hydrogen at high temperatures, as it flows through the second catalyst layer. This gas then flows into the bottom section of the first catalyst layer, where any gas which has not reacted is converted into hydrogen. The generated hydrogen passes through the hydrogen-permeable tube for selective separation and collection. The sweep gas enters the upper part of the annulus created between the hydrogen-permeable tube and the sweep gas tube. The sweep gas and hydrogen flow through the sweep gas tube and out of the hydrogen outlet. The process feed gas is reformed into hydrogen at a high conversion efficiency as it passes through the high temperature second catalyst layer, which is located in the third annulus immediately inside the inner furnace cylinder composing a furnace. The reformed hydrogen is separated and collected through a hydrogen-permeable tube in the second annulus. Any portion of process feed gas which has not reacted is reformed in the first catalyst layer. Thus, the overall conversion efficiency is significantly improved. Furthermore, according to the first and second aspects of this invention, hydrogen is generated in the second catalyst layer, but is not separated or collected through the hydrogen-permeable tubes there. Therefore, the partial pressure of hydrogen in the product gas rises at the outlet of the second catalyst layer; that is, at the inlet of the first catalyst layer. This increases forces to transfer substances to improve the efficiency of separation and collection of hydrogen through the hydrogen-permeable tube in the first catalyst layer. It is therefore possible to reduce the area allotted for gas permeation. Also, when a taller and larger design is adopted for a hydrogen producing apparatus the reforming catalyst layer and the hydrogen-permeable tube also have to be taller. As a result, the difference in thermal expansion between the reforming catalyst layer and the hydrogen-permeable tube becomes significant. The consequent friction between the reforming catalyst layer and the hydrogen-permeable tube may cause the reforming catalyst to become powder due to friction. In conventional hydrogen producing apparatuses, the upper part of the hydrogen-permeable tube is fixed while the lower end is left free, permitting movement at the lower end. This causes notable powdering of the reforming catalyst as it is pressed and destroyed. However, the upper end of the hydrogen-permeable tube in the hydrogen producing apparatus, according to the fifth and seventh aspects of this invention, is free while its lower section is fixed. This eliminates pressure on or destruction of the reforming catalyst for taller hydrogen producing apparatuses, thereby reducing the likelihood of the reforming catalyst powdering as a result of friction. The reforming catalyst layer can therefore be taller than in conventional apparatuses, enabling use of a comparatively low strength reforming catalyst in a large hydrogen producing apparatus. The hydrogen-permeable metallic membrane should preferably be made of a non-porous layer of an alloy containing Pd, V or N, such as: Pd-containing alloys including Pd-Ag alloys, Pd-Y alloys, Pd-Ag-Au alloys; V-containing alloys including V-Ni alloys and V-Ni-Co alloys; and Ni-containing alloys including LaNi 5 alloys. A suitable manufacturing method for the non-porous Pd layer is disclosed in US Patent Nos. 3,155,467 and 2,773,561. In preferable embodiments, a cylindrical radiating body should be placed to surround the frame formed by the combustion burner flame within the inner cylinder. The radiating body radiates heat to raise the temperature of the reforming catalyst layer, and this ensures the required heat flux is available and undesirable partial or uneven heating of the hydrogen-permeable tube is avoided. This also makes it possible to maintain a uniform temperature distribution of the reforming catalyst layer. The temperature of the hydrogen-permeable tube should not be raised above 800°C because of its heat resistance characteristics. The radiating body should preferably have a porous wall so that the combustion gas can flow through the porous wall to efficiently heat the radiating body. A dual arrangement comprising an inner cylindrical radiating body and an outer cylindrical radiating body is preferred as another example of the radiating body arrangement. In the first aspect of this invention, the combustion gas flows down inside the inner cylindrical radiating body, and then up the annulus created by the inner and outer radiating bodies, and down again in a space between the outer cylindrical radiating body and the inner cylinder mentioned above, so as to efficiently heat the radiating bodies. In the second aspect of this invention, the vertical flow of the combustion gas is turned up side down as compared with the first aspect of the invention because the general arrangement of the whole apparatus including the burner is turned that way. In another preferable embodiment for the first aspect of the invention, the radiating body is preferably cylindrical and has an opening in its lower part, and the top of the radiating body is spaced apart from the ceiling of the inner cylinder. In this arrangement, the combustion gas can flow downward inside the radiating body, and a part of the gas flows upward in an annular space defined by the inner cylinder and the radiating body via the opening, and the gas flows down again inside the radiating body via the gap formed between the top of the radiating body and the ceiling of the inner cylinder, so as to circulate the inside and outside of the radiating body. On the other hand, for the second aspects of the invention, the radiating body is preferably cylindrical and has an opening in its upper part, and the bottom of the radiating body is spaced apart from the bottom of the inner cylinder. In such arrangement, the combustion gas can flow upward inside the radiating body, and a part of the gas flows downward in an annular space defined by the inner cylinder and the radiating body via the opening, and the gas flows up again inside the radiating body via the gap formed between the bottom of the radiating body and the bottom of the inner cylinder, so as to circulate the inside and outside of the radiating body. An alternative embodiment of the invention is a column-shaped catalytic combustion apparatus in the inner cylinder in place of the combustion burner. In this case, the catalytic combustion apparatus serves as a combustion burner as well as a radiating body, and can heat the reforming catalyst layer uniformly. BRIEF DESCRIPTION OF THE DRAWINGS Figure 1 is a structural drawing of a conventional laboratory scale apparatus; Figure 2 is a partial sectional view of the hydrogen-permeable tube shown in Figure 2; Figure 3 is a longitudinal sectional view of embodiment 1 according to the first aspect of the invention; Figure 4 is a typical transverse sectional view along the line VI-VI of Figure 3; Figure 5 is a longitudinal sectional view of embodiment 2 of the invention; Figure 6 is a longitudinal sectional view of a modification of embodiment 2 of the invention; Figure 7 is a longitudinal sectional view of another modification of embodiment 2 of the invention; Figure 8 is a longitudinal sectional view of embodiment 3 of the invention; Figure 9 is a longitudinal sectional view of embodiment 4 according to the second aspect of the invention; Figure 10 is a typical transverse sectional view along the line XI-XI in Figure 9; Figure 11 is a longitudinal sectional view of embodiment 5 of the invention; Figure 12 is a longitudinal sectional view of a modification of embodiment 5 of the invention; Figure 13 is a longitudinal sectional view of another modification of embodiment 5 of the invention; and Figure 14 is a longitudinal sectional view of embodiment 6 of the invention. DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENTS As shown in Figure 1, the hydrogen-permeable tube 32 has a closed base and has an external diameter of about 20 mm. It also has an internal support material made of stainless steel mesh 36. An inorganic porous layer 38 made of stainless steel non-woven cloth is disposed around the mesh 36 and acts as a supporting frame for the hydrogen-permeable metal membrane, which is essentially a coated non-porous Pd-based alloy membrane 40. The hydrogen-permeable tubes in each embodiment which will be discussed in the following share a similar structure. Figure 3 is an illustrated sectional view of embodiment 1 for the first aspect of the present invention. Figure 4 is a transverse sectional view at the line VI-VI in Figure 3. The hydrogen producing apparatus 510 is equipped with a closed bottom 512 outermost outer cylinder 514. Within this cylinder is a concentric arrangement consisting of an outer cylinder 516, intermediate cylinder 518 and inner cylinder 520. All four vessels are upright cylinders. The lower sections of the inner cylinder 520 and the outer cylinder 516 are connected, forming a closed annular bottom 522. The outermost outer cylinder 514 and the outer cylinder 516 create the first annulus 524 between their cylinder walls. The bottoms of the first annulus 524 and the inner cylinder space 526 within the inner cylinder 520 are connected. A flow route of the combustion gas starts in the inner cylinder space 526 and passes through a space between the closed bottom 512 of the outermost outer cylinder 514 and the closed annular bottom 522 into the first annulus 524. The outer cylinder 516 and the intermediate cylinder 518 create a second annulus 528 between their cylinder walls. The intermediate cylinder 518 and the inner cylinder 520 create a third annulus 530 between them. The bottoms of the second annulus 528 and the third annulus 530 are connected. The wall of the outermost outer cylinder 514 and the wall of the closed bottom 512 of the outermost external wall 514 are constructed of fire resistant brick. The first and second catalyst layer 528 and 530 (for the sake of convenience the same numerals as the second and third annuluses are used) which are filled with reforming catalyst A in the second annulus 528 and the third annulus 530 are created. Figure 4 shows a large number of cylindrical hydrogen-permeable tubes 532 with hydrogen-permeable metal membranes on an inorganic porous layer, installed vertically around the circumference of the second annulus 528 in the first catalyst layer 528. The cylindrical, stainless steel sweep gas tubes 534 are installed in a concentric manner in the hydrogen-permeable tube 532. As shown in Figure 2, the tubular hydrogen-permeable tube 532 (or 32) has a closed bottom and an external diameter of about 20 mm. The tube contains a supporting material of stainless steel mesh 36. On top of the mesh is an inorganic porous layer 38 of woven stainless steel fabric, which carries the hydrogen-permeable metal membrane. A non-porous, Pd based alloy, hydrogen-permeable metal membrane 40 is coated on top of the fabric. Figure 3 shows that the drooping combustion burner 544 faces downward from the ceiling 542 of the inner cylinder space 526. The combustion burner 544 is connected to a fuel gas tube 544 and air intake tube 547. Figures 3 and 4 support the following discussion of the processes of hydrogen producing apparatus 510. Fuel gas enters the combustion burner 544 via the fuel gas tube 545, and is burnt in air supplied by the air intake tube 547. The prescribed temperature is maintained by supplying to the first and second catalyst 528 and 530 with the heat energy necessary for the steam reforming reaction. Combustion gas passes through the inner cylinder space 526 and the space created by the closed bottom 512 of the outermost outer cylinder 514 and the closed annular bottom 522 and the closed bottom 512. It then travels through the first annulus 524 and exhausts via the combustion gas outlet 546. The process feed gas comprises either light hydrocarbons or a mixture of methanol gas and steam. The gas enters via the raw material gas inlet 548 in the top section of the third annulus 530. It flows into the second catalyst layer 530 of the third annulus 530, during which it is converted into hydrogen at a high temperature. The gas then flows into the bottom of the first catalyst layer 528 of the second annulus 528, where any process feed gas which has not reacted is converted into hydrogen. The generated hydrogen is selectively collected through the hydrogen-permeable tube 532 installed in the first catalyst layer 528 and flows out, with the sweep gas, through the hydrogen outlet 552 in the top section of the tube. The sweep gas enters via the sweep gas inlet 550 in the top section of the apparatus. The gas flows down the annulus 533 between the sweep gas tube 534 and the hydrogen-permeable tube 532, sweeps the hydrogen, and enters the lower end opening of the sweep gas tube 534. The gas and hydrogen move upward through the sweep gas tube and flow out of the hydrogen outlet 552. This process suppresses the partial pressure of hydrogen on the after-permeation side of the hydrogen-permeable tube 532. Generated CO and CO 2 gas, plus any raw material gas which has not reacted after passing through the first catalyst layer 528, flow out of the system via the off gas outlet 554. In this embodiment, the process feed gas passes through the high temperature heated catalyst layer 530 immediately inside the inner cylinder 520 which forms the furnace. After the gas is reformed into hydrogen at a high conversion rate, the hydrogen is selectively collected through the hydrogen-permeable tube in the second annulus 528. Any process feed gas which has not reacted is reformed in the reforming catalyst layer 528 in the second annulus 528, significantly improving the conversion efficiency for the entire apparatus. Figures 5 and 6 illustrate embodiment 2. Figure 5 shows an inner cylinder space 626 of the hydrogen producing apparatus 660 which contains a cylindrical radiating body 662 surrounding the drooping combustion burner 644 flame. This cylindrical radiating body 662 has porous walls. The combustion burner 644 gas permeates the porous wall and flows into the inner cylinder space 626. The combustion gas heats the radiating body 662 during this process, resulting in a uniform overall temperature. The heated radiating bodies 662 evenly heats the reforming catalyst layer 630, with almost uniform heat flux. The hydrogen producing apparatus 660 in Figure 6 is a modification of the radiating bodies 662 shown in Figure 25. The radiating body assembly 662 shown in Figure 6 has a dual cylinder configuration and comprises an inner cylinder radiating body 664 and an outer cylinder radiating body 666. The inner cylinder radiating body 664 is in contact with the ceiling 642 of the inner cylinder 620, but has gaps between it's bottom and the closed bottom 612 of the outermost outer cylinder 614. The outer cylinder radiating body 666 is in contact with the closed bottom 612, and its upper section is isolated from the ceiling 642. The combustion burner 644 gas flows down through the inner cylindrical radiating body 664, then moves upward through the annulus 667 between the inner cylindrical radiating body 664 and the external radiating body 666. The gas flows from the upper part of the outer cylindrical radiating body 666 into the inner cylinder space 626. The combustion gas heats up the inner cylinder radiating body 664 and the outer cylinder radiating body 666 during this process, achieving a uniform overall temperature. The heated internal radiating body 664 and external radiating body 666 heat the reforming catalyst layer 630 with an almost uniform heat flux. The hydrogen producing apparatus 660 shown in Figure 7 is another modification of the radiating bodies 662 in Figure 5. The cylindrical radiating bodies 662 shown in Figure 7 are constructed of fire resistant bricks. There is a gap 668 between the upper section of the radiating bodies 662 and the ceiling 642 of the hydrogen producing apparatus 660, and an opening 670 in the lower section of the radiating bodies 662. The combustion gas flows down through the radiating bodies 662 from the drooping combustion burner 644, and out through an opening 670 in the lower section. A portion of the combustion gas moves up through the annulus 672 between the inner cylinder 620 and the radiating bodies 662, and returns to the radiating body 662 via the gap 668. The combustion gas thoroughly heats the radiating bodies 662 during this process, resulting in an almost uniform overall temperature. The heated radiating bodies 662 evenly heat the reforming catalyst layer 630, with almost uniform heat flux. The hydrogen producing apparatus 680 in Figure 8 is a modification of the apparatus 510 in Figure 3. The apparatus 680 contains a column shaped catalyst burner 682 in the inner cylinder space 626, instead of a combustion burner. The catalyst burner 682 comprises an internal tube 684 which delivers the fuel gas and air and a mesh external tube 686 to surround the internal tube. A combustion catalyst layer 688 fills the space between the two tubes. The fuel gas is burnt in the combustion catalyst layer 688 and heats the overall catalyst burner 682 to a uniform temperature. The heated catalyst burner 682 evenly heats the reforming catalyst layer 630, with almost uniform heat flux. A specific example for the fourth aspect of the invention will be described in the following. (1) Apparatus Structure Figure 3 shows a hydrogen producing apparatus 510. The reaction apparatus in Figure 3 has an effective length of 600 mm and is structured as: inner cylinder 520 (internal diameter 100 mm); intermediate cylinder 518 (internal diameter 118 mm); outer cylinder 516 (internal diameter 175 mm); outermost outer cylinder 514 (internal diameter 190 mm); hydrogen-permeable tube 532 (external diameter 20 mm); and sweep gas tube 534 (external diameter 6 mm). Fifteen upright hydrogen-permeable tubes 532 are installed in the first catalyst layer of the second annulus 528 in an equidistant manner around the circumference. Reforming catalyst A is a nickel based catalyst (average particle size: 2 mm in diameter). The furnace comprises a drooping burner 544, as shown in Figure 3. The outermost outer cylinder 514 is insulated with 200 mm thick rockwool to reduce heat discharge to the external atmosphere. (2) Operating Conditions Supply of raw material gas (town gas 13A) on the reformer side: 32.1 mole/h Steam supplied in raw material gas on the reformer side: 1.35 kg/h Steam for reforming/raw material gas on the reformer side (mole ratio): 2.0 Reforming reaction temperature: 550°C Reforming reaction pressure: 6.03 kgf/cm 2 -abs. Quantity of sweep gas (steam) supplied: 1.41 kg/h Sweep gas pressure: 1.22 kgf/cm 2 -abs. (3) Hydrogen Generation Test Results A reaction under these above conditions produces 123.0 mole/h of hydrogen, accompanied by sweep gas. CO impurity in the hydrogen is less than 1 ppm. The conversion efficiency of hydrocarbons in the raw material gas is about 90%. In contrast, a conventional reformer which does not use a hydrogen-permeable tube is hampered by chemical equilibrium, based on the relationship between operating temperature and pressure, resulting in a conversion efficiency of about 24% at this reaction temperature and pressure. The fourth aspect of the invention facilitates industrial-scale hydrogen production, economically producing high purity hydrogen, and has the following advantages: (a) The structure is simple and compact, comprising multiple layered cylinders. The apparatus can be constructed with a small quantity of materials. (b) The heat capacity of the apparatus is small, as it is far lighter in weight than conventional multiple parallel reaction tube systems. The operation of the apparatus can be started and stopped quickly, and it has an excellent response to load changes. (c) The catalyst layer can be more uniformly heated, as heat is applied from both sides. Radial thermal flux distribution is more uniform because of the structure of layered cylinders with a central furnace. This prevents the development of hot spots where temperature may exceed the limit the hydrogen-permeable tubes can withstand. (d) Hydrogen is only generated in the second catalyst layer and is not separated or collected through the hydrogen-permeable tube there. The partial pressure of hydrogen in the generation gas therefore rises at the second catalyst layer outlet or the first catalyst layer inlet. This raises the substance transfer propulsion force for the separation and collection of hydrogen by the hydrogen-permeable tube in the first catalyst layer. It is therefore possible to reduce the area of permeation and achieve an improved separation efficiency. (e) The collection efficiency of the generated hydrogen is improved by the counter-flow substance transfer between sweep gas in the hydrogen-permeable tube and the reformed gas in the catalyst layer. (f) Separating and collecting the hydrogen through the hydrogen-permeable tube shifts the chemical equilibrium to the advantage of hydrogen production. The reforming temperature can therefore be reduced 150-200°C below that of conventional systems. As a consequence, carbon dialysis in the reforming catalyst layer is eased and the steam/hydrocarbon ratio (mole ratio) can be reduced from a standard value of 3 to 2-2.2. This vastly improves thermal efficiency while reducing the thermal energy required to heat raw material gas. (g) The lower reaction temperature enables the use of inexpensive materials with lower heat resistance characteristics, thereby reducing construction costs. (h) Radiating bodies ensure the catalyst layer to be heated with a uniform temperature distribution without any risk of overheating. Figure 9 is an illustrated sectional view of embodiment 4 for the hydrogen producing apparatus according to the second aspect of the invention. Figure 10 is a transverse sectional view at the line XI-XI in Figure 9. The hydrogen producing apparatus 1010 is equipped with a covered outermost outer cylinder 1014 with a ceiling 1012. Within this cylinder is a concentric arrangement consisting of an outer cylinder 1016, intermediate cylinder 1018 and inner cylinder 1020. All four vessels are upright cylinders. The upper sections of the inner cylinder 1020 and the outer cylinder 1016 are connected, forming a closed annulus with a connected top 1022. The walls of the outermost cylinder 1014 and the outer cylinder 1016 create the first annulus 1024. The top sections of the first annulus 1024 and the inner cylinder space 1026 are connected. A flow route or the combustion gas starts in the inner cylinder space 1026 and passes through a space between the ceiling 1012 of the outermost cylinder 1014 and the connected top annulus 1022 into the first annulus 1024. The walls of the outer cylinder 1016 and the intermediate cylinder 1018 create a second annulus 1028. The walls of the intermediate cylinder 1018 and the inner cylinder 1020 create a third annulus 1030. The bottoms of the second annulus 1028 and the third annulus 1030 are connected. The wall of the outermost outer cylinder 1014 and the ceiling wall 1012 of the outermost outer cylinder 1014 are constructed of fire resistant brick. The first and second catalyst layer 1028 and 1030 (for the sake of convenience the same numerals as the second and third annuluses are used) which are filled with reforming catalyst A in the second annulus 1028 and the third annulus 1030 are created. Figure 10 shows a large number of cylindrical hydrogen-permeable tubes 1032 with hydrogen-permeable metal membranes on an inorganic porous layer, installed vertically around the circumference of the second annulus 1028 in the first catalyst layer 1028. The cylindrical, stainless steel sweep gas tubes 1034 are installed in a concentric manner in the hydrogen-permeable tube 1032. As shown in Figure 2, the tubular hydrogen-permeable tube 1032 (or 32) has a closed end and an external diameter of about 20 mm. The tube contains a supporting material made of stainless steel mesh 36. On top of the mesh is an inorganic porous layer 38 of woven stainless steel fabric, which carries the hydrogen-permeable metal membrane. A non-porous, Pd based alloy, hydrogen-permeable metal membrane 40 is coated on top of the fabric. Figure 9 shows that the upright combustion burner 1044 faces upward from the bottom 1042 of the inner cylinder space 1026. The combustion burner 1044 is connected to a fuel gas tube 1045 and air intake tube 1047. Referring to Figures 9 and 10, the processes of hydrogen producing apparatus 1010 will be described in the following. The fuel gas enters the combustion burner 1044 via the fuel gas tube 1045, and is burnt in air supplied by the air intake tube 1047. The prescribed temperature is maintained by supplying to the first and second catalyst 1028 and 1030 the heat energy necessary for the steam reforming reaction. Combustion gas passes through the space in the inner cylinder 1026 and the space created by the ceiling 1012 of the outermost outer cylinder 1014 and the annular connection section 1022. The gas then moves through the first annulus 1024 and exhausts via the combustion gas outlet 1046. The process feed gas comprises either light hydrocarbons or a mixture of methanol gas and steam. The gas enters via the raw material gas inlet 1048 in the lower section of the third annulus 1030. It flows into the third annulus 1030 and up through the second catalyst layer 1030, where it is converted into hydrogen at a high temperature. It then flows into the top of the first catalyst layer 1028 of the second annulus 1028, where any process feed gas which has not reacted is converted into hydrogen. The generated hydrogen is selectively collected through the hydrogen-permeable tube 1032 installed in the first catalyst layer 1028 and flows, with the sweep gas, through the hydrogen outlet 1052 in the lower section of the tube. The sweep gas is fed from the sweep gas inlet 1050 in the lower part of the apparatus. The gas flows up through the dual tube space 1033 between the sweep gas tube 1034 and the hydrogen-permeable tube 1032, and flows into the open top end of the sweep gas tube 1034, sweeping the hydrogen as it moves. The gas and generated hydrogen fall and flow out of the hydrogen outlet 1052. By removing the hydrogen with sweep gas, the partial pressure of hydrogen on the after-permeation side of the hydrogen-permeable tube 1032 is suppressed. Steam and inert gas can be used as sweep gas. The generated CO and CO 2 , plus any raw material gas which has not reacted after passing through the first catalyst layer 1028, exit the system via the off gas outlet 1054. In this embodiment, the process feed gas passes through the high temperature catalyst layer 1030 in the inner cylinder 1020 which forms the furnace. The gas is reformed into hydrogen at a high conversion rate, and is selectively collected through the hydrogen-permeable tube 1032 in the second annulus 1028. Any process feed gas which has not reacted is reformed in the reforming catalyst layer 1028 of the second annulus 1028, significantly improving the conversion efficiency for the entire apparatus. Referring to Figures 11 to 13, embodiment 5 will be described. Only those parts of these figures which are different from the hydrogen producing apparatus illustrated in Figures 9 and 10 will be explained. The inner cylinder space 1026 of hydrogen producing - apparatus 1010 of Figure 11 contains a cylindrical radiating body 1062 surrounding the upright combustion burner 1044 flame. This cylindrical radiating body 1062 has porous walls. The combustion burner 1044 gas permeates the porous wall and flows into the inner cylinder space 1026. The combustion gas heats the radiating body 1062 during this process, resulting in a uniform overall temperature. The heated radiating bodies 1062 evenly heat the reforming catalyst layer 1030, with almost uniform heat flux. The hydrogen producing apparatus 1010 in Figure 12 is a modification of the radiating bodies 1062 of Figure 11. The radiating body assembly 1062 shown in Figure 12 has a dual cylinder configuration and comprises an inner cylinder radiating body 1064 and outer cylinder radiating body 1066. The inner cylinder radiating body 1064 is in contact with the bottom 1042 of the inner cylinder 1020, but has gaps between it's upper part and the ceiling 1012 of the outermost outer cylinder 1014. The outer cylinder radiating body 1066 is in contact with the upper part of the ceiling 1012, and its lower section is separated from the bottom 442. The combustion burner 1044 gas flows up through the internal radiating body 1064, then moves downward through the annulus 1067 between the internal radiating body 1064 and the external radiating body 1066. The gas flows from the lower part of the external radiating body 1066 into the inner cylinder space 1026. The combustion gas heats up the inner cylinder radiating body 1064 and the outer cylinder radiating body 1066 during this process, achieving a uniform overall temperature. The heated internal radiating body 1064 and external radiating body 1066 heat the reforming catalyst layer 1030 with an almost uniform heat flux. The hydrogen producing apparatus 1010 in Figure 13 illustrates another modification of the radiating body 1062 in Figure 14. The radiating body 1062 in Figure 13 is cylindrical, and constructed of fire resistant brick. There is a opening 1068 between the lower section of the radiating body 1062 and the bottom 1042 of the hydrogen producing apparatus 1010. The upper section of the radiating body 1062 has a gap 1070 which is separated from the ceiling 1012 of the outermost cylinder 1014. The combustion gas flows up from the upright combustion burner 1044 though the radiating body 1062, and is emitted from the gap 1070 in the upper section. A portion of the combustion gas moves down in the annulus 1072 between the inner cylinder 1020 and the radiating body 1060, and circulates by flowing into the radiating body 1062, via the opening 1068. The temperature of the radiating body 1062 is maintained at a uniform level by this process. The heated radiating body 1062 heats the reforming catalyst layer 1030 in an even manner, with almost uniform heat flux. The hydrogen producing apparatus 1010 in Figure 14 is a modification (embodiment 6) of the hydrogen producing apparatus 1010 in Figure 9. In this instance, a column shaped catalyst burner 1082 is installed in the inner cylinder space 1026 instead of a combustion burner. The catalyst burner 1082 comprises a porous internal tube 1084 to introduce fuel gas and air, a mesh external tube 1086 surrounding the internal tube, and a combustion catalyst layer 1088 between these tubes. Fuel gas burnt in the combustion catalyst layer 1088 heats the catalyst burner 1082 to a uniform temperature. The heated catalyst burner 1082 heats the reforming catalyst layer 1030 in an even manner, with almost uniform heat flux. A specific example for the seventh aspect of the invention will be described in the following. (1) Apparatus Structure Figure 9 shows a hydrogen producing apparatus 1010. The reaction apparatus in Figure 9 has an effective length of 600 mm and is structured as: inner cylinder 1020 (internal diameter 100 mm); intermediate cylinder 1018 (internal diameter 118 mm); outer cylinder 1016 (internal diameter 175 mm); outermost outer cylinder 1014 (internal diameter 190 mm); hydrogen-permeable tube 832 (external diameter 20 mm); and sweep gas tube 1034 (external diameter 6 mm). Fifteen upright hydrogen-permeable tubes 32 are installed in the first catalyst layer of the second annulus 1028 in an equidistant manner around the circumference. Reforming catalyst A is a nickel based catalyst (average particle size: 2 mm in diameter). The furnace comprises an upright burner 1044, as shown in Figure 9. The outermost outer cylinder 1014 is insulated with 200 mm thick rockwool to reduce heat discharge to the external atmosphere. (2) Operating Conditions Supply of raw material gas (town gas 13A) on the reformer side: 32.1 mole/h Steam supplied in raw material gas on the reformer side: 1.35 kg/h Steam for reforming/raw material gas on the reformer side (mole ratio): 2.0 Reforming reaction temperature: 500°C Reforming reaction pressure: 6.03 kgf/cm 2 -abs. Quantity of sweep gas (steam) supplied: 1.41 kg/h Sweep gas pressure: 1.22 kgf/cm 2 -abs (3) Hydrogen Generation Test Results A reaction under these conditions produces 123.0 mole/h of hydrogen, accompanied by sweep gas. CO impurity in the hydrogen is less than 1 ppm. The conversion efficiency of hydrocarbons in the raw material gas is about 90%. In contrast, a conventional reformer which does not use a hydrogen-permeable tube is hampered by chemical equilibrium, based on the relationship between operating temperature and pressure, resulting in a conversion efficiency of 24% at this reaction temperature and pressure. Based on the above structures, the second aspect of the invention facilitates industrial-scale hydrogen production, economically producing high purity hydrogen, and has the following advantages: (a) The upward facing flame of the upright burner improves the stability of the flame and enables the construction of a larger hydrogen producing apparatus. This structure also supports significant changes in processing quantity in one large apparatus. (b) The lower section of the hydrogen-permeable tube is fixed, while its upper part is free. This reduces catalyst powdering caused by friction between the hydrogen-permeable tube and the reforming catalyst layer occurring as a result of thermal expansion. This structure also eliminates destruction of the reforming catalyst caused by pressure in the lower part of the layer which occurs when the upper section of the hydrogen-permeable tube is fixed. It is therefore possible to use reforming catalysts of relatively low strength and construct larger apparatuses by making the reforming catalyst layer taller. This hydrogen producing apparatus according to the second aspect of the invention has the above-mentioned advantages over conventional apparatuses with drooping combustion burners. In addition to the above mentioned advantages, the seventh aspect of the invention offers the following benefits which are common with corresponding apparatuses with drooping combustion burners. (c) The structure is simple and compact, comprising multiple layered cylinders. The apparatus can be constructed with a small quantity of materials. (d) The heat capacity of the apparatus is small, as it is far lighter in weight than conventional multiple parallel reaction tube systems. The operation of the apparatus can be started and stopped quickly, and it has an excellent response to load changes. (e) The catalyst layer can be more uniformly heated, as heat is applied from both sides. Radial thermal flux distribution is more uniform because of the structure of layered cylinders with a central furnace. This prevents the development of hot spots where temperature may exceed the limit the hydrogen-permeable tubes can withstand. (f) The second catalyst layer generates hydrogen but does not separate or collect it through a hydrogen-permeable tube. As a result the partial pressure of hydrogen in the generated gas rises at the outlet of the second catalyst layer, that is, at the inlet of the first catalyst layer. The consequent substance transfer propulsion force for the separation and collection of hydrogen by the hydrogen-permeable tube in the first catalyst layer enables the permeation area to be reduced as a result of the increased separation speed. (g) The generated hydrogen collection efficiency is improved by the counter-flow substance transfer between the sweep gas in the hydrogen-permeable tube and the reformed gas in the catalyst layer. (h) Separating and collecting the hydrogen through the hydrogen-permeable tube shifts the chemical equilibrium to the advantage of hydrogen production. The reforming temperature can therefore be reduced 150-200°C below that of conventional systems. (i) The lower reaction temperature enables the use of inexpensive materials with lower heat resistance characteristics, thereby reducing construction costs. (j) Radiating bodies ensure the catalyst layer to be heated with a uniform temperature distribution without any risk of overheating.

Claims: A hydrogen producing apparatus (510, 1010) in which hydrogen produced from a steam reforming reaction in a fixed bed catalyst is separated and collected by passing through a partitioning wall having selective permeability for hydrogen, said apparatus comprising: an outermost outer cylinder (514, 1014) having a closed bottom (512, 1012) at one end thereof; an outer cylinder (516, 1016) in said outermost outer cylinder (514, 1014) in coaxial spaced relationship thereto to form a first annulus (524, 1024) therebetween; an intermediate cylinder (518, 1018) in said outer cylinder (516, 1016) in coaxial spaced relationship thereto to form a second annulus (528, 1028) therebetween; an inner cylinder (520, 1020) in said intermediate cylinder (518, 1018) in coaxial spaced relationship therewith to form a third annulus (530, 1030) therebetween and having an inner cylinder space (526, 1026), the inner cylinder (520, 1020) and the outer cylinder (516, 1016) being joined together at one end of each in spaced relationship to said closed bottom (512, 1012) of said outermost outer cylinder (514, 1014) to form a closed annular bottom (522, 1022) of said second and third annulus (528, 1028, 530, 1030); a combustion burner (544, 644, 1044) disposed substantially in said inner cylinder space (526, 626, 1026) and said second and third annulus (528, 1028, 530, 1030); wherein said first annulus (524, 1024) is in communication with said inner cylinder space, and said second annulus (528, 1028) is in communication with said third annulus (530, 1030); first and second catalyst layers of reforming catalyst in the second and third annulus (528, 1028, 530, 1030), respectively; at least one hydrogen-permeable tube (532, 1032) having a hydrogen-permeability, the hydrogen-permeable tube (32) being disposed in said first catalyst layer in said second annulus (528, 1028) and having an open end and a closed end adjacent said closed annular bottom (522, 1022); a sweep gas tube (534, 1034) disposed within said at least one hydrogen-permeable tube (532, 1032) and having an open inlet end proximate said closed end of said at least one hydrogen-permeable tube (532, 1032) and an outlet end, said hydrogen after selective separation flowing as a product gas through said open end of said sweep gas tube (534, 1034), through said sweep gas tube, and out of said apparatus through said outlet end of said sweep gas tube, remaining raw material gas and product gas flow at least partly in counter-flowing relation with respect to each other on opposite sides of a wall of the hydrogen-permeable tube (532, 1032); a raw material gas inlet (548, 1048) for conducting raw material gas to the third annulus (530, 1030), which flows through said second catalyst layer, so that the gas which flows through said second catalyst layer, is converted into hydrogen at a high temperature, and subsequently the raw material gas is conducted into the first catalyst layer so that an unreacted portion of the gas is converted into hydrogen, said hydrogen permeates said at least one hydrogen-permeable tube (532, 1032) and is selectively separated thereby; and an off gas outlet (554, 1054) communicating with said second annulus (528, 1028) for discharging said remaining raw material gas after separation of hydrogen therefrom. The apparatus claimed in claim 1, wherein at least one cylindrical radiating body (662, 1062) is disposed inside said inner cylinder space (626, 1026) so as to surround said combustion burner (1044). The apparatus claimed in claim 2, wherein at least one radiating body has a dual cylindrical structure which comprises an outer cylinder radiating body (666, 1066) and an inner cylindrical radiating body (664, 1064) disposed in coaxial spaced relationship within the outer cylinder radiating body to provide an annular space (667, 1067) therebetween, said inner and outer cylinder radiating bodies being supported in said inner cylinder space (626, 1026) so that combustion gas from said combustion burner (644, 1044) flows in the direction of the flame of said combustion burner in said inner cylinder radiating body, then in an opposite direction from said direction of flame in said annular space between said inner and outer cylinder radiating bodies, and then in the same direction as said flame in an annular space between said outer cylinder radiating body (666, 1066) and said inner cylinder (620, 1020). The apparatus claimed in claim 2, wherein said at least one radiating body is cylindrical; said at least one radiating body (662, 1062) has an open end which is in spaced relationship to a ceiling (642, 1042) which defines said inner cylinder space (626, 1026) and has said combustion burner (644, 1044); and said at least one radiating body has another end which has at least one opening (670, 1070) therein communicating with said inner cylinder space (626, 1026) adjacent said bottom section (612, 1012) of said outermost outer cylinder (614, 1014) ; wherein combustion gas from said combustion burner flows in the direction of the flame of said burner inside said radiating body (662, 1062), through said at least one opening (670, 1070) in said radiating body, and a part of said combustion gas flows in the direction opposite from said direction of flame in an annular space between said inner cylinder (626, 1026) and said at least one radiating body (662, 1062) and through a space (668, 1068) between said open end of said radiating body and said ceiling (642, 1042) which defines said inner cylinder space (626, 1026) and which has said combustion burner (644, 1044), and then again in said direction of the flame inside said at least one radiating body, the combustion gas circulating inside and outside said radiating body (662, 1062). The apparatus claimed in claims 2 or 4, wherein said radiating body (662, 1062) comprises a porous wall. The apparatus claimed in anyone of claims 1 to 5, wherein the flow direction of said product gas and that of said raw material gas are reversible from the respective flow directions. The apparatus claimed in any one of claims 1 to 6, wherein a source of sweep gas is provided, and the sweep gas is suppliable to said at least one hydrogen-permeable tube (532, 1032), respectively, so as to sweep said product gas out of the apparatus (510, 1010) through said inlet and outlet ends of said sweep gas tube (534, 1034). The apparatus claimed in any one of claims 1 to 6, wherein a suction pump having an inlet connectable to said outlet end of said sweep gas tube (534, 1034) or said hydrogen-permeable tube (532, 1032) is provided so as to conduct said product gas out of the apparatus (510, 1010). The apparatus claimed in any one of claims 1 to 8, wherein the hydrogen-permeable tube (532, 1032) comprises an inorganic porous layer and a hydrogen-permeable metal membrane which is non-porous thin film made of an alloy containing at least one element chosen from the group consisting of Pd, Ni, and V and which is supported on said inorganic porous layer. The apparatus claimed in any one of claims 1 to 9, comprising a column-shaped catalyst burner portion in said inner cylinder space (526, 626, 1026) inside said inner cylinder (520, 1020) instead of a combustion burner. The apparatus claimed in any one of claims 1 to 10, wherein said closed bottom (512, 612) of said outermost outer cylinder (514) forms the bottom of the apparatus (510, 660). The apparatus claimed in any one of claims 1 to 10, wherein said closed bottom (1012) of said outermost outer cylinder (1014) forms the ceiling of the apparatus (1010).

Inventors: FUJIMOTO YOSHIMASA, GONDAIRA MASAYUKI, KOBAYASHI KAZUTO, KURODA KENNOSUKE, MAKIHARA HIROSHI, OHTA SHINSUKE, OHTA YOSHU, SHIRASAKI YOSHINORI, UCHIDA HIROSHI, UCHIDA TOSHIYUKI, FUJIMOTO, YOSHIMASA, GONDAIRA, MASAYUKI, KOBAYASHI, KAZUTO, KURODA, KENNOSUKE, MAKIHARA, HIROSHI, OHTA, SHINSUKE, OHTA, YOSHU, SHIRASAKI, YOSHINORI, UCHIDA, HIROSHI, UCHIDA, TOSHIYUKI, FUJIMOTO, YOSHIMASA, C/O MITSUBISHI JUKOGYO K.K., KOBAYASHI, KAZUTO, C/O MITSUBISHI JUKOGYO K.K., KURODA, KENNOSUKE, C/O MITSUBISHI JUKOGYO K.K., MAKIHARA, HIROSHI, C/O MITSUBISHI JUKOGYO K.K., OHTA, SHINSUKE, C/O MITSUBISHI JUKOGYO K.K., UCHIDA, TOSHIYUKI, C/O MITSUBISHI JUKOGYO K.K.
Applicants: MITSUBISHI HEAVY IND LTD, TOKYO GAS CO LTD, MITSUBISHI JUKOGYO KABUSHIKI KAISHA, TOKYO GAS CO., LTD.
Application year: 1994
Main classification: C01B3
IPC codes: B01J8, C01B3, H01M8